U.S. patent application number 10/227690 was filed with the patent office on 2003-06-12 for methods for controlling screenouts.
Invention is credited to Boney, Curtis L., Miller, Matthew J..
Application Number | 20030106690 10/227690 |
Document ID | / |
Family ID | 26921669 |
Filed Date | 2003-06-12 |
United States Patent
Application |
20030106690 |
Kind Code |
A1 |
Boney, Curtis L. ; et
al. |
June 12, 2003 |
Methods for controlling screenouts
Abstract
Methods are presented to induce a screenout during a
subterranean formation fracturing or combined fracturing and gravel
packing treatment by laying down a filter cake early in the
treatment, then injecting proppant slurry, and then while proppant
slurry injection continues chemically damaging the filter cake with
one or more filter cake degradation agents so that leak-off
increases, the concentration of proppant in the fracture increases,
and the proppant screens out. The additional use of filter cake
degradation agent aids and bridging-promoting materials is
included.
Inventors: |
Boney, Curtis L.; (Houston,
TX) ; Miller, Matthew J.; (Missouri City,
TX) |
Correspondence
Address: |
SCHLUMBERGER TECHNOLOGY CORPORATION
IP DEPT., WELL STIMULATION
110 SCHLUMBERGER DRIVE, MD1
SUGAR LAND
TX
77478
US
|
Family ID: |
26921669 |
Appl. No.: |
10/227690 |
Filed: |
August 26, 2002 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
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60334703 |
Oct 31, 2001 |
|
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|
Current U.S.
Class: |
166/280.1 ;
166/308.3 |
Current CPC
Class: |
C09K 8/703 20130101;
C09K 8/62 20130101; Y10S 507/924 20130101; C09K 8/74 20130101 |
Class at
Publication: |
166/280 ;
166/308 |
International
Class: |
E21B 043/267 |
Claims
We claim:
1. A method of causing a screenout in a subterranean formation
stimulation treatment, comprising injecting a slurry of a proppant
in a carrier fluid above fracturing pressure to create one or more
fractures, comprising: a) forming a filter cake, and b) degrading
the filter cake with a filter cake degradation agent while
injecting a slurry of a proppant in a carrier fluid.
2. The method of claim 1 wherein the filter cake comprises the
viscosifying agent in the carrier fluid.
3. The method of claim 2 wherein the viscosifying agent in the
carrier fluid is selected from the group consisting of
water-soluble polymers and crosslinked water-soluble polymers.
4. The method of claim 1 wherein the filter cake comprises a fluid
loss additive.
5. The method of claim 4 wherein the fluid loss additive is
selected from the group consisting of water-soluble polymers,
crosslinked water-soluble polymers, asbestos, starch, calcium
carbonate, mica, plastic particles, solid wax, wax-polymer
particles, insoluble salts, slowly soluble salts, and mixtures
thereof, provided that at least one component can be broken or
dissolved.
6. The method of claim 1 wherein the filter cake degradation agent
is selected from the group consisting of oxidizers, enzymes, acids
and mixtures thereof.
7. A method of causing a screenout in a subterranean formation
stimulation treatment, comprising injecting a slurry of a proppant
in a carrier fluid above fracturing pressure to create one or more
fractures, comprising the steps of: a) injecting a pad fluid that
forms a filter cake, b) injecting one or more first slurry stages
comprising a proppant in a carrier fluid; and c) degrading the
filter cake with a filter cake degradation agent while injecting
one or more second slurry stages comprising a proppant in a carrier
fluid.
8. The method of claim 7 wherein the pad fluid comprises a member
of the group consisting of fluid loss additives, filter cake
degradation agents, filter cake degradation agent aids, and
mixtures thereof, provided that no filter cake degradation agent
aid is included for a filter cake degradation agent that is
included.
9. The method of claim 7 wherein the one or more first slurry
stages comprise a member of the group consisting of fluid loss
additives, filter cake degradation agents, filter cake degradation
agent aids, and mixtures thereof, provided that no filter cake
degradation agent aid is included for a filter cake degradation
agent that is included or was in the pad.
10. The method of claim 8 wherein the one or more first slurry
stages comprise a member of the group consisting of fluid loss
additives, filter cake degradation agents, filter cake degradation
agent aids, and mixtures thereof, provided that no filter cake
degradation agent aid is included for a filter cake degradation
agent that is included or was in the pad.
11. The method of claim 7 wherein the one or more second slurry
stages comprise a member of the group consisting of filter cake
degradation agents, filter cake degradation agent aids, and
mixtures thereof.
12. The method of claim 8 wherein the one or more second slurry
stages comprise a member of the group consisting of filter cake
degradation agents, filter cake degradation agent aids, and
mixtures thereof.
13. The method of claim 9 wherein the one or more second slurry
stages comprise a member of the group consisting of filter cake
degradation agents, filter cake degradation agent aids, and
mixtures thereof.
14. The method of claim 10 wherein the one or more second slurry
stages comprise a member of the group consisting of filter cake
degradation agents, filter cake degradation agent aids, and
mixtures thereof.
15. The method of claim 14 wherein the pad fluid and the one or
more first slurry stages each comprise a fluid loss additive, a
first filter cake degradation agent and a filter cake degradation
agent aid for a second filter cake degradation agent that is more
active under treatment conditions than is the first filter cake
degradation agent; and the one or more second slurry stages contain
the second filter cake degradation agent.
16. The method of claim 15 wherein the filter cake comprises a
polymer subject to enzymatic and oxidative degradation under
treatment conditions; the first filter cake degradation agent is
present in the pad and comprises an enzyme that degrades the
polymer; the second filter cake degrading agent is present in the
one or more second slurry stages and comprises an oxidizing
compound that degrades the polymer; and the second filter cake
degradation agent aid for the second filter cake degradation agent
is present in the pad fluid, the one or more first slurry stages,
and the one or more second slurry stages and comprises a tertiary
amine.
17. The method of claim 14 wherein the filter cake comprises an
acid-soluble solid particulate compound and the second filter cake
degrading agent is present in the one or more second slurry stages
and comprises an acid capable of dissolving at least part of the
acid-soluble solid particulate compound under treatment
conditions.
18. The method of claim 14 wherein one or more of the pad fluid,
the one or more first slurry stages, and the one or more second
slurry stages comprise a bridging-promoting material.
19. The method of claim 18 wherein the pad fluid comprises a
bridging-promoting material.
20. The method of claim 18 wherein the pad fluid and the one or
more first slurry stages comprise a bridging-promoting
material.
21. The method of claim 18 wherein the pad fluid, the one or more
first slurry stages, and the one or more second slurry stages
comprise a bridging-promoting material.
22. The method of claim 18 wherein the one or more first slurry
stages comprise a bridging-promoting material.
23. The method of claim 18 wherein the one or more first slurry
stages, and the one or more second slurry stages comprise a
bridging-promoting material.
24. The method of claim 18 wherein the one or more second slurry
stages comprise a bridging-promoting material.
25. The method of claim 7 wherein one or more of the pad fluid, the
one or more first slurry stages, and the one or more second slurry
stages comprise a member of the group consisting of fluid loss
additives, filter cake degradation agents, filter cake degradation
agent aids, bridging-promoting materials, and mixtures thereof.
26. The method of claim 1 wherein a sand control screen is in place
before the treatment.
27. The method of claim 7 wherein a sand control screen is in place
before the treatment.
28. The method of claim 18 wherein a sand control screen is in
place before the treatment.
29. The method of claim 1 further comprising the step of gravel
packing at least a portion of the wellbore in the producing
formation.
30. The method of claim 7 further comprising the step of gravel
packing at least a portion of the wellbore in the producing
formation.
31. The method of claim 18 further comprising the step of gravel
packing at least a portion of the wellbore in the producing
formation.
32. The method of claim 26 further comprising the step of gravel
packing at least a portion of the wellbore in the producing
formation.
33. The method of claim 27 further comprising the step of gravel
packing at least a portion of the wellbore in the producing
formation.
34. The method of claim 28 further comprising the step of gravel
packing at least a portion of the wellbore in the producing
formation.
Description
REFERENCE TO RELATED PROVISIONAL APPLICATION
[0001] This application claims the benefit of provisional
application serial No. 60/334,703 filed Oct. 31, 2001.
TECHNICAL FIELD OF THE INVENTION
[0002] This Invention relates to increasing the flow of fluids into
or out of subterranean wells. More particularly it relates to
stimulation of the flow of fluids from the rock of a formation into
a wellbore. Most particularly it relates to methods of controlling
the size and shape, location, and quality of fractures created in
hydraulic fracturing (either conventional or with coiled tubing),
or in fracturing and gravel packing in one operation, or in gravel
packing.
BACKGROUND OF THE INVENTION
[0003] Hydraulic fracturing, gravel packing, or fracturing and
gravel packing in one operation, are used extensively to stimulate
the production of hydrocarbons, water and other fluids from
subterranean formations. These operations involve pumping a slurry
of "proppant" in hydraulic fracturing (natural or synthetic
materials that prop open a fracture after it is created) or
"gravel" in gravel packing. In high permeability formations, the
goal of a hydraulic fracturing treatment is typically to create a
short, wide, highly conductive fracture, in order to bypass
near-wellbore damage done in drilling and/or completion, to ensure
good communication between the rock and the wellbore and to
increase the surface area available for fluids to flow into the
wellbore. Gravel is also a natural or synthetic material, which may
be identical to, or different from, proppant. Gravel packing is
used for "sand" control. Sand is the name given to any particulate
material, such as clays, from the formation that could be carried
into production equipment. Gravel packing is a sand-control method
used to prevent production of formation sand, in which a steel
screen is placed in the wellbore and the surrounding annulus is
packed with prepared gravel of a specific size designed to prevent
the passage of formation sand that could foul subterranean or
surface equipment and reduce flows. The primary objective of gravel
packing is to stabilize the formation while causing minimal
impairment to well productivity. Sometimes gravel packing is done
without a screen. High permeability formations are frequently
poorly consolidated, so that sand control is needed. Therefore,
hydraulic fracturing treatments in which short, wide fractures are
wanted are often combined in a single continuous ("frac and pack")
operation with gravel packing. For simplicity, in the following we
may refer to any one of hydraulic fracturing, fracturing and gravel
packing in one operation (frac and pack), or gravel packing, and
mean them all.
[0004] It is very undesirable to allow the proppant or gravel to
pack the wellbore above the producing formation. If this happens,
the wellbore must be cleaned out to permit various other downhole
operations, such as placement of tools, to permit optimal fluid
production. It is also very undesirable if the operation screens
out too late or not at all, that is if the fracture keeps growing,
in length and/or in height, beyond what is necessary and desired,
and an optimal pack and desired fracture size and shape are never
generated to maximize production and to prevent flowback of
proppant or sand.
[0005] As mentioned, short, wide fractures are often desired. The
most common method of creating short-wide fractures is to initiate
a tip screenout during the pumping operation. In a tip screenout,
the solids concentration at the tip of the fracture becomes so high
due to fluid leak-off into the formation that the slurry is no
longer mobile. The concentrated proppant slurry plugs the fracture,
and prevents additional fracture growth. Additional pumping of the
proppant/fluid slurry into the formation after the screenout causes
the fracture to grow wider, and large concentrations of proppant
per surface area are placed in the fracture. The design of these
treatments relies heavily on knowing the correct mechanical
properties, permeability, reservoir pressure and fluid saturations
of the formation being treated. Prior to most of these treatments a
small fracturing treatment (sometimes called a "data frac" or
"mini-frac") is performed in order to measure these properties and
to determine the formation's response to a hydraulic fracturing
treatment. Treatment designs are often modified on the fly to
incorporate this new information. Important design parameters are
the size of the pad, the size and number of stages, and the
proppant or gravel concentration in each subsequent stage, and the
nature of the fluid and additives used in each stage. Treatment
design and modification is typically done with the aid of a
computer model, many of which are available in the industry.
[0006] The pad is the proppant-free fluid pumped to initiate and
propagate a fracture before stages including proppant or gravel are
started. It typically serves another purpose as well. It lays down
a coating, called a "filter cake", on the faces of the forming
fracture. This filter cake reduces the flow of fluid from the
fracture into the formation (affecting the "efficiency" of the job
(see below)). The filter cake may be formed from the viscosifying
agents that are normally present, such as polymers. The filter cake
may also be formed by adding additional materials to the fluid for
that purpose, especially if the pores in the fracture face are
large. Such optionally added materials in this use are often called
fluid loss control additives, or FLA's.
[0007] In hydraulic fracturing, in particular in low permeability
formations where the longest possible fracture is desired (in order
to create the largest possible fracture face for flow of fluids
into the fracture and ultimately into the wellbore), modes of
operation that might induce a tip screenout are typically avoided,
in order to achieve long, conductive fractures. If a tip screenout
is encountered in such a fracturing operation before the entire
designed treatment is pumped, as inferred from an increase in
pumping pressure, the pump rate is reduced or most likely the
treatment is stopped and considered a failure. We will call
hydraulic fracturing job designs and job executions in which a tip
screenout is not desired and does not occur, "conventional"
hydraulic fracturing.
[0008] On the other hand, sometimes tip screenouts are desired.
Design features typically employed in those special situations in
which a tip screenout is desired typically involve methods of
ensuring that fluid leak-off is high relative to the rate and
amount of proppant injection. This can be achieved by using a small
pad, using little or no fluid loss additive, using higher proppant
concentrations earlier in the treatment, pumping more slowly, and
other methods known to those skilled in the art of fracturing and
combined fracturing/gravel packing.
[0009] Unfortunately, in spite of data-fracturing information, the
pressure transients collected by downhole pressure gauges during
treatments indicate that TSO's do not occur in many, perhaps the
majority, of the treatments in which they are desired and intended.
The fluid at the tip of the fracture remains mobile, the fracture
tip continues to grow throughout the treatment and the desired
proppant concentration in the fracture is not reached. Therefore,
the desired fracture conductivity is not obtained. Often, TSO's
have to be coaxed by lowering pump rates or increasing proppant
concentrations when the TSO is desired.
[0010] There are two principal reasons for not achieving an
appropriate TSO. First, the fracture may be too large for the
proppant volume. This occurs a) when the pad is too large or b)
when the "efficiency" is too high, or c) when the ratio of proppant
volume to slurry volume selected in the design of the job is not
high enough. (The "efficiency" in a fracturing operation is high
when fluid leak-off is controlled--either naturally by the
properties of the fluid and the matrix, or by the addition of fluid
loss control additives--to an acceptably low level; efficiency is
low when leak-off is high, so that very large volumes of fluid must
be pumped in order to generate the intended fracture size and shape
and to place a specified amount of proppant or gravel.) Second, the
fracture width may be too great for the proppant to form a bridge
in the fracture. This may be due to bad initial design (for example
in choice of proppant diameter) or to width growth beyond what was
expected.
[0011] Up until now, besides designing the job better, the major
way to deal with these problems was directed towards optimizing the
choice of fluid loss control additive or additives and the stages
of the job in which they were used, especially if the main problem
was that the fracture was too large for the proppant volume.
[0012] Fibers are used in fracturing to control proppant flowback.
In that case, fiber is added at an optimal concentration to control
proppant flowback, while not significantly impacting fracture
conductivity. If one is using glass fibers, for example, this
concentration is approximately 1 weight per cent by weight of the
proppant. This concentration is insufficient to cause bridging
during pumping under the conditions at which it is normally
employed, especially in low permeability formations. Fibers are
also used sometimes to aid in transport of proppant when the
viscosity of the fluid is very low. Tip screenout is commonly
deliberately avoided in these treatments; proppant concentrations
are kept low through careful pre-treatment job design, especially
in careful selection of pumping schedules. For example, in these
treatments the pad volume is increased over conventional job
designs to ensure that sufficient fracture width is generated prior
to the proppant/fiber slurry entering the fracture. However, U.S.
patent application Ser. No. 10/214,817 (assigned to Schlumberger
Technology Corporation, filed Aug. 8, 2002, hereby incorporated in
its entirety by reference) describes a method of deliberately using
fibers to enhance tip screenout when desired.
[0013] The ability to achieve success in obtaining TSO's is very
uncertain in significant part due to the fact that the true nature
of the subterranean formation is unknown and variable. It would be
highly desirable if a method were available to induce a TSO when
needed that depends more upon features of the job under the
operator's control (especially the chemistry of the fluids and
fluid loss control additives used) than on the unknown variability
of the formation. There is a need for a more reliable way to ensure
that intended tip screenouts will occur and to allow for more
flexibility in design of tip screenout treatments.
SUMMARY OF THE INVENTION
[0014] One embodiment of the Invention is a method of causing a
screenout, during stimulation of a subterranean formation by
propped fracturing, by forming a filter cake and then degrading the
filter cake with a filter cake degradation agent while injecting
proppant slurry into the fracture. In some embodiments the filter
cake is formed from the viscosifier for the carrier fluid in the
slurry or from a fluid loss additive or both. In some embodiments
the filter cake degradation agent may be an oxidizer, an enzyme, an
acid or mixtures of these. Another embodiment is a method of
causing a screenout in a subterranean formation stimulation
treatment, including injecting a slurry of a proppant in a carrier
fluid above fracturing pressure to create one or more fractures,
the method including the steps of injecting a pad fluid that forms
a filter cake; injecting one or more first slurry stages comprising
a proppant in a carrier fluid; and degrading the filter cake with a
filter cake degradation agent while injecting one or more second
slurry stages comprising a proppant in a carrier fluid. In other
embodiments of this method, the pad fluid includes one or more than
one of fluid loss additives, filter cake degradation agents, filter
cake degradation agent aids, and mixtures thereof, provided that no
filter cake degradation agent aid is included for a filter cake
degradation agent that is included; the one or more first slurry
stages include one or more than one of fluid loss additives, filter
cake degradation agents, filter cake degradation agent aids, and
mixtures thereof, provided that no filter cake degradation agent
aid is included for a filter cake degradation agent that is
included or was in the pad; and the one or more second slurry
stages include one or more than one of filter cake degradation
agents, filter cake degradation agent aids, and mixtures thereof.
In another embodiment, the pad fluid and the one or more first
slurry stages each include a fluid loss additive, a first filter
cake degradation agent and a filter cake degradation agent aid for
a second filter cake degradation agent that is more active under
treatment conditions than is the first filter cake degradation
agent; and the one or more second slurry stages contain the second
filter cake degradation agent. In another embodiment, the filter
cake includes a polymer subject to enzymatic and oxidative
degradation under treatment conditions; the first filter cake
degradation agent is present in the pad and includes an enzyme that
degrades the polymer; the second filter cake degrading agent is
present in the one or more second slurry stages and includes an
oxidizing compound that degrades the polymer; and the second filter
cake degradation agent aid for the second filter cake degradation
agent is present in the pad fluid, the one or more first slurry
stages, and the one or more second slurry stages and is a tertiary
amine. In another embodiment the filter cake includes an
acid-soluble solid particulate compound and the second filter cake
degrading agent is present in the one or more second slurry stages
and includes an acid capable of dissolving at least part of the
acid-soluble solid particulate compound under treatment conditions.
In another embodiment one or more of the pad fluid, the one or more
first slurry stages, and the one or more second slurry stages
include a bridging-promoting material. In a preferred embodiment,
the filter cake includes a polymer subject to enzymatic and
oxidative degradation under treatment conditions; the first filter
cake degradation agent is present in the pad and includes an enzyme
that degrades the polymer; the second filter cake degrading agent
is present in the one or more second slurry stages and includes an
oxidizing compound that degrades the polymer; the second filter
cake degradation agent aid for the second filter cake degradation
agent is present in the pad fluid, the one or more first slurry
stages, and the one or more second slurry stages and is a tertiary
amine; and at least some of the one or more first slurry stages
contain a bridging-promoting material. In other embodiments, a sand
control screen is in place before the treatment. In other
embodiments, the treatment is a combined fracturing/gravel packing
treatment.
BRIEF DESCRIPTION OF THE FIGURES
[0015] FIG. 1 shows typical fluid leak-off volume data with and
without a fluid loss additive.
[0016] FIG. 2 is a schematic of the depth of penetration of
leaked-off fluid into a formation with and without a leak-off
additive.
[0017] FIG. 3 shows dynamic fluid loss volume and fluid viscosity
vs. a time function in experiments with two different combinations
of FLA, filter cake degradation agents, and a filter cake
degradation agent aid.
[0018] FIG. 4 shows dynamic fluid loss volume and fluid viscosity
vs. a time function in an experiment in which addition of FLA is
stopped and there is no filter cake degradation agent or filter
cake degradation agent aid.
[0019] FIG. 5 is a schematic showing the effect on fracture
generation of adding an FLA, fiber, filter cake degradation agents,
and a filter cake degradation agent aid.
DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
[0020] To aid in understanding deliberate tip screenouts promoted
by job design in hydraulic fracturing and combined fracture/gravel
packing operations, see M. Economides and K. Nolte, eds., Reservoir
Stimulation, 3.sup.rd edition, John Wiley & Sons, Ltd, New York
(2000) pp 10-21 to 10-24; and F. L. Monus, F. W. Broussard, J. A.
Ayoub and W. D. Norman, "Fracturing Unconsolidated Sand Formations
Offshore Gulf of Mexico," SPE 24844, (1992). We have now found ways
to bring about screenouts in a fracture deliberately and in a
controlled manner by manipulation of the composition of the
injected fluids. One method is particularly effective when the
failure to screen out is due to the fracture being too large for
the proppant volume; this method is to form a filter cake and then
to reduce the amount of filter cake, or increase its permeability,
at the appropriate time. We will use the term filter cake
degradation to encompass reducing the amount of filter cake or
increasing its permeability by breaking or dissolving at least a
portion of at least one of the components of the filter cake. This
is done, for example, by breaking or dissolving the filter cake
during the job with one or more appropriate breakers or dissolvers,
which we will term filter cake degradation agents, sometimes with
an additional breaker or dissolver aid, which we will term a filter
cake degradation agent aid. The breakers or dissolvers may be
delayed, for example with delay agents or by encapsulation. When
the fracture is too large for the proppant volume, one or more
breakers or dissolvers may be added throughout the job or at least
in the pad and/or early stages of the job.
[0021] Other methods are particularly effective when the failure to
screen out is due primarily to the fracture being too wide for the
proppant to bridge. An example is to reduce the efficiency in the
later stages of the job by adding an appropriate breaker, sometimes
with a breaker aid, in the later stages of the job, or by adding
more breaker or a better breaker in the later stages of the job. In
this embodiment, breaker may not have been used in the pad or in
the early proppant stages. These breakers are effective when the
filter cake's resistance to fluid flow results primarily from
polymers in the fluid or in the FLA.
[0022] If the filter cake's resistance to fluid flow results
primarily from calcium carbonate or one or more other acid-soluble
materials in the FLA, the filter cake can be dissolved by adding
acid to the later stages.
[0023] Another method is to add fibers or other materials (termed
bridging-promoting materials) with the proppant to assist in
bridging, in conjunction with one of the above methods of breaking
or dissolving the filter cake.
[0024] The methods involving breaking or dissolving the filter cake
and adding fibers can be combined, simultaneously or consecutively.
These methods can also be used to form wider fractures (that have
grater fracture conductivity) deliberately. These methods can also
be used as a form of diversion, that is the operator can
deliberately stop the growth and packing of one fracture and
initiate a new fracture without zonal isolation. The methods can be
used to destroy the FLA throughout the fracture or only in part of
it. The operator can decide and control when and where the
screenout occurs (and avoid the undesirable results of failure to
screen out, of very gradual and inefficient screenout, or of
screenout in the wellbore above the formation) by accelerating the
leak-off, optionally also by assisting bridging.
[0025] The underlying and unifying concept is that a filter cake is
laid down early in the treatment, then proppant slurry is injected,
and then while proppant slurry injection continues the filter cake
is chemically damaged by a filter cake degradation agent so that
leak-off increases, the concentration of proppant in the fracture
increases, and the proppant screens out. Depending upon such
factors as the reactivity under the treatment conditions (for
example temperature and carrier fluid pH) of the filter cake
degradation agent or agents used, the thickness of the filter cake
deposited (affected for example by the carrier fluid viscosity and
the formation permeability) and other job design parameters such as
the planned duration of the job, dimensions of the fracture, and
proppant particle size, the timing of the addition of various
chemicals will vary. For example, the pad must be pumped long
enough and/or contain enough FLA to ensure laying down the needed
filter cake. The filter cake degradation must not be so fast, or be
begun so soon, that screenout occurs before it is wanted.
Conversely, the filter cake degradation must not be so slow, or be
begun so late, that screenout does not occur or occurs too late.
Proppant addition is usually done in stages. In each stage a
certain proppant concentration is injected for a certain amount of
time. Successive stages usually have successively increasing
proppant concentrations. The proppant concentration may also be
ramped smoothly, that is increase continuously during the
proppant-laden stages. To aid in description, a typical job will be
broken up into the pad and two sets of proppant slurry stages. In
the pad, the fracture is initiated and filter cake is laid down. In
the first set of stages, the fracture is enlarged. In the second
set of stages, a screenout occurs and the fracture is packed with
proppant. As was said, certain other features of the job may
strongly influence the timing of the addition of the chemicals. If
the pad must be small, laying down of filter cake may continue in
all of, or the early stages of, the first set of stages. If the
filter cake degradation agent is slow acting, addition may begin
even in the pad, and degradation may begin in the first set of
stages. If it is very fast acting, addition may begin only in the
second set of stages. Filter cake degradation agents of
successively increasing reactivity may be used, or filter cake
degradation agents that degrade different components of the filter
cake may be used simultaneously or successively. If the filter cake
degradation agent is not reactive enough a filter cake degradation
agent aid may be added. That filter cake degradation agent aid may
be added before or after the filter cake degradation agent is
added, in such a way that both are present only in the second set
of stages, or they may both be added together in the second set of
stages. A bridging-promoting agent may be added in any or all of
the pad and stages. One skilled in the art of subterranean
formation stimulation could design treatments that generate a
fracture having specific final parameters (such as dimensions and
conductivity) in many different ways within the scope and spirit of
the Invention, depending upon such factors as, for example, the
availability of chemicals and materials; the availability and
capability of the equipment with which the chemicals and materials
can be added; and cost.
[0026] The Invention is preferably carried out by first considering
information about the well, the formation, the fluids available,
and criteria for a successful fracture stimulation, and preparing
an optimized plan for maximizing stimulated well performance
according to the data and the criteria. Such a design will include
injection of an amount of a selected pad fluid and an amount of a
selected fracture fluid. This is usually done by analyzing the well
using fracturing design and evaluation software in which pressure
gradients are combined with fracture length and height evolution
algorithms, complete leak-off information, and the effects of
multiple fluid injections and their temperature changes. For
hydraulic fracturing or gravel packing, or a combination of the
two, aqueous fluids for pads or for forming slurries are
viscosified with polymers (usually crosslinked with a boron,
zirconium or titanium compound), or with viscoelastic surfactants
("VES's") that can be formed using certain surfactants that form
appropriately sized and shaped micelles. Any fracture or gravel
packing fluids can be used in the Invention, provided that they are
compatible with the special materials of the Invention (FLA's,
fibers, breakers, breaker aids), and with the formation, the
proppant, and the desired results of the treatment. Thus the fluid
can for example be aqueous based or oil-based, acidic or basic, and
can comprise one or more polymers, viscoelastic surfactants, or
gelled oils. The polymers may be crosslinked. The methods of the
Invention can be incorporated into the original job design or the
job could be designed without planning a TSO and then it could be
decided during the job execution that a TSO was desired and the job
could be modified on the fly accordingly. (Note that in this
description, we often refer to any screenout in the fracture as a
tip screenout (TSO), but by TSO we mean a screenout that occurs in
the fracture and not necessarily at the very end of the fracture
farthest from the wellbore; what is critical is that the screenout
occurs when and where it is desired and not in the wellbore.)
[0027] We shall use the term "conventional fracturing" here to
refer to hydraulic fracturing in which a tip screenout is neither
intended nor desired. We shall use the term "tip screenout" to mean
a screenout that is in the fracture and not in the wellbore, but is
not necessarily in the end of the fracture away from the wellbore.
In conventional fracturing, modes of operation that might induce a
tip screenout are avoided. If a tip screenout is encountered in a
conventional fracturing operation, as inferred from an increase in
pumping pressure, before the entire designed treatment is pumped,
some change may be made on the fly in the job parameters, for
example pump rate or proppant concentration, to try to minimize the
tendency toward tip screenout. Frequently, however, the treatment
is stopped and considered to be a failure.
[0028] The pad of the Invention comprises a carrier fluid and a
viscosifying polymer or a VES. It may additionally contain other
additives normally used in such fluids, provided that none of the
components of the pad is deleterious to the formation or to the
fracture fluid. Fluids used as the pad in the present Invention may
typically contain materials such as corrosion inhibitors, friction
reducers, clay stabilizers, scale inhibitors, biocides, and the
like.
[0029] The carrier fluid provides a medium for the transport of the
other components into the formation. Preferably, the carrier fluid
is water or brine. Selected organic or inorganic salts or mixtures
can be included, provided that they are compatible with all
components in the pad, the fracture fluid, the formation and the
formation fluids. Solutions containing from about 1 to about 7% by
weight potassium chloride (KCI) or ammonium chloride are often used
as the base liquid in fracturing fluids and pads to stabilize clays
and prevent clay swelling. Sometimes other brines or seawater may
be used. An organic cation salt, such as, in particular, tetra
methyl ammonium chloride, is an effective salt, especially but not
limited to about 0.2 to about 0.5 percent by weight.
[0030] Typically, if a polymer is used to viscosify the fluids, the
polymer is water-soluble. Common classes of effective water-soluble
polymers include polyvinyl polymers, polymethacrylamides, cellulose
ethers, polysaccharides, lignosulfonates, and ammonium, alkali
metal, and alkaline earth salts thereof. Specific examples of
typical water soluble polymers are acrylic acid-acrylamide
copolymers, acrylic acid-methacrylamide copolymers,
polyacrylamides, partially hydrolyzed polyacrylamides, partially
hydrolyzed polymethacrylamides, polyvinyl alcohol, polyvinly
acetate, polyalkyleneoxides, carboxycelluloses,
carboxyalkylhydroxyethyl celluloses, hydroxyethylcellulose,
galactomannans (e.g., guar gum), substituted galactomannans (e.g.,
hydroxypropyl guar, carboxymethyl hydroxypropyl guar, and
carboxymethyl guar), heteropolysaccharides obtained by the
fermentation of starch-derived sugar (e.g., xanthan gum), and
ammonium and alkali metal salts thereof. Preferred water-soluble
polymers include hydroxyethyl cellulose, starch, scleroglucan,
galactomannans, and substituted galactomannans.
[0031] The optimal polymer concentration can be determined by
choosing the desired leak-off parameters and measuring leak-off
with samples of the intended fluids and of the formation or of a
rock similar to the formation. Leak-off is defined by three terms:
"spurt", which is the initial rapid leak-off of fluid before a
filtercake barrier is formed on the fracture face and is measured
in gallons/100 square feet, and, for the subsequent leak-off that
occurs even after a filtercake is formed and is governed by the
viscosity and the wall-building propensity: Cw, the wall-building
fluid loss coefficient, and Cv, the viscosity controlled fluid loss
coefficient. Cw is not applicable where there is no wall-building
material present. Cv is not applicable where there is a low, finite
Cw. Cw and Cv are measured in ft/min.sup.1/2. Preferred values of
spurt, Cw and Cv respectively are 0 to about 5, about 0.001 to
about 0.05, and about 0.001 to about 0.05; more preferred values
are 0 to about 2, about 0.001 to about 0.008, and about 0.001 to
about 0.008; most preferred values are 0 to about 1, about 0.001 to
about 0.003, and about 0.001 to about 0.003. The values of these
parameters (and the actual behavior they represent) can vary
significantly provided that a suitable filter cake is produced in
an appropriate time. A test method for determining these values is
given in Navarrete, R. C., Caweizel, K. E., and Constien, V. G.:
"Dynamic Fluid Loss in Hydraulic Fracturing Under Realistic Shear
Conditions in High-Permeability Rocks," SPE Production and
Facilities, pp 138-143 (August, 1996).
[0032] Any VES based fluid can be used, in or after the pad, that
is compatible with the formation, the formation fluids, and any
additives. Particularly effective fluids are those described in
U.S. Pat. Nos. 5,551,516; 5,964,295; 5,979,555; 5,979,557;
6,140,277; and 6,258,859, all hereby incorporated by reference.
Breakers may also be used for VES's.
[0033] Since the methods of the Invention work primarily by the
properly timed and located destruction or weakening of a filter
cake, the pad and/or the proppant carrying stages preferably also
contain a fluid loss control additive or additives to form a
suitable filter cake. If they do not contain polymeric materials
that can form a suitable filter cake, for example if the fracturing
pad and/or carrier fluid are viscosified with a VES, then the pad
and/or the proppant carrying stages must contain a fluid loss
control additive or additives to form a suitable filter cake. Fluid
loss additives can be, by non-limiting example, water-soluble
polymers or crosslinked water-soluble polymers. If the pad and/or
proppant laden fluids are viscosified with a polymer or
cross-linked polymer, the FLA may be the same or a different
polymer or crosslinked polymer. The amount needed to viscosify the
carrier fluid may be adequate or more may be added to form an
appropriate filter cake. FLA's can also be solids such as asbestos,
granular starch, calcium carbonate (calcite), particulate mica,
plastic particles, solid wax or wax-polymer particles, solid
oil-soluble resin particles, insoluble salts, slowly soluble salts
(such as sodium chloride if the carrier fluid and formation water
have high ionic strengths), and mixtures thereof. The FLA must
contain at least one component that can be broken or degraded (for
example oxidation of a polymer, or enzymatic degradation of a
cross-linked natural polymer) or dissolved (for example dissolution
of calcium carbonate by an acid, or dissolution of a wax or resin
by a solvent).
[0034] The Invention is carried out by determining, sometimes first
by experiment and usually finally by computer simulation and
modeling, the optimal amounts of FLA and breaker or breakers
(optionally with breaker aid) or dissolver (such as acid), and the
stages in which they should be included so that the filter cake
breaks or dissolves at the desired time and place. One skilled in
the art of stimulation of subterranean wells and formations can
readily do this with a knowledge of the chemicals and conditions
(especially time and temperature) involved. The process can be done
for example by adjusting the chemistry and/or the job pumping
design or both, including iteratively, usually by modeling until
the desired result is predicted. We will call the materials used to
break or dissolve filter cakes and/or FLA's "filter cake
degradation agents". In some embodiments an FLA may not have been
added and the filter cake may have been formed by the viscosifying
agent only. In other embodiments, for example when the fluid is
viscosified with a VES, the filter cake may have been formed
entirely from the FLA or FLA's. In one preferred embodiment, the
pad, and optionally the first proppant-laden stages, contain a
first breaker and a breaker aid (which could for example be a
catalyst) for a second breaker. Subsequent stages contain the
second breaker. The breakers and breaker aids can be solids or
liquids, and can be delayed (for example by encapsulation).
Intermediate stages could contain both breakers or both breakers
plus the breaker aid for the second breaker, or only the second
breaker and its breaker aid. Thus the filter cake already contains
a breaker aid for the second breaker when the second breaker
contacts the filter cake. Thus, the various stages of the job (pad,
early proppant stages, late proppant stages) can contain various
combinations of FLA, different breakers, and breaker aids for the
different breakers. A breaker aid could be pumped before, with, or
after the breaker for which it is active. A material that forms a
filter cake will always be in the pad, either the viscosifying
agent (polymer or crosslinked polymer) or an added FLA. Breaker
does not necessarily have to be in the pad, especially if the
temperature is high enough for at least some natural degradation to
occur. Similarly, an FLA does not necessarily have to be in all of
the proppant-containing stages, or any of the proppant-containing
stages, if a satisfactory filter cake has already been formed. All
of these methods are counter to normal practice, in which it is
desirable to maintain fluid efficiency as high as possible until
the stimulation job is done.
[0035] If the filter cake is to be degraded by dissolution of a
component (such as but not limited to calcium carbonate), this can
be done by using an acid in the polymer, crosslinked polymer, or
VES (all of which are known in the art in combination with acids)
in the appropriate stage or stages. Appropriate acids are any acids
known in the art for dissolving carbonates, such as, but not
limited to, mineral acids like hydrochloric acid, hydrofluoric
acid, and mixtures of the two. Organic acids, such as, but not
limited to formic acid, acetic acid, fluoboric acid, and citric
acid, can also be used, in conjunction with the mineral acids or
separately. Additional materials, such as chelating agents, may be
used to enhance the dissolution by the acid. Non-limiting examples
are aminopolycarboxylic acids such as ethylenediamine tetraacetic
acid, diethylenetriamine pentaacetic acid, and mixtures
thereof.
[0036] This use of acids to dissolve the filter cake during a
fracturing job is opposite to what is normally done in conventional
fracturing, in which removal of the filter cake during the job is
undesirable. For example, there are known methods for acid
fracturing in which pad and acid stages are alternated. Each pad
stage contains an FLA or polymer or emulsion that forms a filter
cake that blocks off regions of the matrix that have already been
etched by the acid (or in which wormholes have formed) and diverts
the acid to a portion of the matrix that has not previously been
attacked by the acid. In such applications, filter cake removal by
the acid is undesirable.
[0037] It is normally desirable for the filter cake to degrade
after stimulation applications in order to reduce the fracture face
"skin" damage and to provide maximal flow of fluids from the matrix
into the fracture and ultimately into the wellbore. This
degradation normally occurs naturally, albeit slowly, by thermal
processes, or by dissolution of the filter cake in typical slurry
fluids, or by physical processes, in particular due to the reversal
of flow (during the treatment flow is out of the fracture and into
the formation, and after production begins the flow is out of the
formation and into fracture). Filter cake degradation agents have
not been used previously to induce very rapid filter cake
degradation during hydraulic fracturing treatments. Because
deliberate degradation of the filter cake by the methods of the
Invention can bring about much faster degradation, it brings about
much faster increase in fluid production rates.
[0038] If the use of fibers is also planned to aid in inducing a
TSO, the fiber is usually in at least the first proppant stages and
the concentration is chosen so that the fiber/proppant slurry packs
off (is no longer mobile) and causes a TSO when the degradation of
the filter cake has proceeded to the point where the fluid
efficiency is less than for example about 20%. Note that the amount
of fiber needed to cause a TSO in the methods of this Invention can
be less than the amount of fiber normally used in fracturing to
prevent proppant flowback without causing a TSO because in the
methods of this Invention, other steps are taken to degrade the
filter cake and increase the concentration of the fiber/proppant
slurry in the fracture. In other words, bridging is promoted by
deliberately enhancing the leak-off. On the other hand, the amount
of fiber used may also be more than that normally used for
preventing proppant flowback.
[0039] The treatment is performed in the usual way with the usual
equipment, chemicals, and personnel, but with the equipment
modified to give the ability to add fiber, or other
bridging-promoting material, if that ability is not already present
and if one of the embodiments to be used involves the addition of
fiber. Methods of adding fiber are described in U.S. Pat. Nos.
5,501,275; and 5,782,300. A preferred, but not limiting, method of
adding fiber is to add it to the fluid at the same time as the
addition of the proppant. Although we have used the term "fiber,"
other materials could also be used as bridging-promoting materials,
such as needles, fibrillated fibers, platelets, and ribbons,
especially materials with aspect ratios greater than about three.
Any organic or inorganic, natural or synthetic, material is
suitable that would decrease the mobility of a fluid/proppant
slurry as it dewaters. Fibers with aspect ratios greater than about
three would be more effective when mixed with proppants because
they would tend to leave a proppant pack with a greater
permeability.
[0040] Fiber, or other bridging-promoting material, may be added in
a sufficiently high concentration to induce a tip screenout, as
described in U.S. Patent Application "Methods and Fluid
Compositions Designed to Cause Tip Screenouts," Dean M Willberg and
Curtis L. Boney, filed Aug. 8, 2002, hereby incorporated by
reference, serial number not yet assigned, which has a common
assignee as the present application. However, bridging-promoting
materials need not be added in an amount sufficient to cause a tip
screenout in the present Invention, when they are used. The
densities of fibers, proppants and fluids each can vary, so the
amount of fiber that will be high enough to induce a tip screenout,
alone or in conjunction with a filter cake degradation agent,
depends upon the specific choices of fibers, proppants and fluids.
The following discussion will be in terms of aqueous liquids and
preferred fibers of the Invention, synthetic organic polymeric
fibers having relatively low densities of from about 1 to about 1.5
grams/cubic centimeter. However, denser fibers, such as those made
from inorganic materials such as glass or ceramics, can also be
used; such fibers will have densities of up to double or more the
densities of synthetic organic polymeric fibers. The amount of
fiber in a liquid/fiber/proppant slurry necessary to induce a tip
screenout when used in conjunction with a filter cake degradation
agent is most closely related to the volume of fiber per volume of
fiber/proppant mixture. Thus the amounts of fiber expressed below
should be adjusted for the densities of the specific components
involved. The higher the density of the fiber, the higher the
necessary weight concentration. Also, the aspect ratio, the length,
and the diameter of the fiber relative to the diameter of a
proppant will affect the amount of fiber (expressed in weight per
cent of liquid in the slurry) in a liquid/fiber/proppant slurry
necessary to induce a tip screenout. A lower weight per cent of
fiber (expressed in weight per cent of liquid in the slurry) will
be necessary as the fiber diameter is decreased or the fiber length
or aspect ratio are increased. These adjustments are well within
the ability of those skilled in the art. Particularly suitable, but
not limiting, fibers and other materials are described in U.S. Pat.
Nos. 5,330,005; 5,439,055; 5,501,275; and 5,782,300, which are
hereby incorporated by reference.
[0041] What we term "fibers" can be any fibrous material, such as
natural organic fibers, synthetic organic fibers (by non-limiting
example polyaramide or polyamide or novoloid or a novoloid-type
polymer), fibrillated synthetic organic fibers, glass fibers,
carbon fibers, ceramic fibers, inorganic fibers, metal filaments or
mixtures thereof. The fibrous material preferably has a length of
about 2 to about 30 nanometers and a diameter of about 10 to about
100 microns, most preferably a length of about 2 to about 30
nanometers and a length of about 10 to about 100 microns. Fiber
cross-sections need not be circular and fibers need not be
straight. If fibrillated fibers are used, the diameters of the
individual fibrils can be much smaller than the aforementioned
fiber diameters. However, as the fracture fluid/fiber/proppant
mixture enters the formation, the proppant and fiber will
concentrate due to fluid leak-off. At higher concentrations the
fiber greatly increases the slurry's propensity to bridge. When the
fiber concentration is increased to about 4 to about 5 weight per
cent by leak-off, the slurry has an appearance of wet pulp. It has
been shown in the laboratory and in yard tests that about 4 to
about 5 per cent synthetic organic polymer fiber in the liquid can
plug a slot 6 to 12 millimeters wide. Therefore, as the fiber and
proppant are concentrated in the fracture due to fluid leak-off,
the slurry will have a great propensity for the proppant/fiber
mixture to bridge and cause a screenout.
[0042] The amount of synthetic organic polymer fiber is preferably
adjusted over the range from about 0.5 to about 2 weight per cent
to account for variations in fluid efficiency. Normally, 0.5 weight
percent synthetic organic polymer fiber would not be considered
high and would not cause a screenout. However, one object of the
Invention is to use a fiber concentration that would result in a
screenout. In some cases, for example if the fluid leak-off
coefficient is relatively high, and the fluid efficiency low, then
the initial fiber concentration could be reduced to about that
amount. The concentration might then be in the "normal" range for a
"normal" treatment, but it would be high for the treatment in
question. On the other hand, if the fluid efficiency were to be
unusually high, then the initial fiber concentration should be
increased beyond the typical 2 per cent to induce a tip screenout.
Thus the range of synthetic organic polymer fiber concentration of
the Invention is from about 0.5 weight per cent of the liquid to
about 3 weight per cent, preferably from about 1 weight per cent to
about 2 weight per cent. In this context, by "high concentration"
we mean a concentration of a specific fiber, in a specific
liquid/fiber/proppant combination, high enough to very
significantly increase the probability of a screenout under the
conditions of the treatment.
[0043] Although in conventional hydraulic fracturing the amount of
fiber used is normally determined by the amount of proppant used,
so that the amount of fiber is changed if the amount of proppant is
changed in different stages, in the fluids and methods of this
Invention the amount of fiber used is more commonly determined by
the amount of liquid used and it is more common to use a constant
amount of fiber by weight of liquid.
[0044] As fiber stiffness or rigidity increases, so does the
propensity to initiate bridging and screenout. However, fluid
handling will become more difficult as stiffness increases. Fibers
of varying stiffness or rigidity are readily available
commercially. Furthermore, friction pressure during pumping often
decreases due to the addition of fibers. This is an added benefit
particularly in combined fracturing/gravel packing operations where
the fluid is often pumped through small ports and passages. The
choice of fiber can readily be made by one of ordinary skill in the
art by considering the various advantages and disadvantages of
different fibers as regards to cost, availability, concentration
needed, ease of handling, effect on friction pressure and other
factors.
[0045] Although we have referred to "tip screenouts" it would be
within the scope of the Invention to generate a desired length of
conventional fracture with conventional treatment parameters and
then induce screenout by beginning addition of filter cake
degradation agent and/or filter cake degradation agent aid at high
concentration and/or by increasing the fiber concentration. Fiber
may also be added to the pad, in amounts comparable to the amounts
added to proppant-laden stages. Although fracturing followed by
gravel packing is more commonly performed with a screen in place,
it is within the scope of the Invention to apply the fluids and
methods to treatments that are done without a screen. Although we
have described the Invention in terms of hydrocarbon production, it
is within the scope of the Invention to use the fluids and methods
in wells intended for the production of other fluids such as water
or brine, and in injection, production, or storage wells. Although
we have described the Invention in terms of unfoamed fluids, fluids
foamed or energized (for example with nitrogen, carbon dioxide or
mixtures thereof) may be used; adjustment to the fiber
concentration due to any consequent changes in the fluid properties
or proppant concentration would be made. It is also to be
understood that the fluids and methods of the Invention may be used
to cause tip screenouts in multiple fractures, natural fractures,
or wormholes or the like created by treatment with acid. Any of the
methods of the Invention can be carried out with coiled tubing.
[0046] Any proppant (gravel) can be used, provided that it is
compatible with the filter cake degradation agent and the
bridging-promoting materials if the latter are used, the formation,
the fluid, and the desired results of the treatment. Such proppants
(gravels) can be natural or synthetic, coated, or contain
chemicals; more than one can be used sequentially or in mixtures of
different sizes or different materials. Proppants and gravels in
the same or different wells or treatments can be the same material
and/or the same size as one another and the term "proppant" is
intended to include gravel in this discussion. In general the
proppant used will have an average particle size of from about 10
to about 100 U. S. mesh, more particularly, but not limited to
40/60, 20/40, 16/20, 12/20 and 8/20 sized materials. Normally the
proppant will be present in the slurry in a concentration of from
about 1 PPA to about 25 PPA, preferably from about 1 to about 12
PPA. (PPA is "pounds proppant added" per gallon of liquid.)
[0047] Any additives normally used in such treatments may be
included, again provided that they are compatible with the other
components and the desired results of the treatment. Such additives
can include, but are not limited to anti-oxidants, crosslinkers,
corrosion inhibitors, delay agents, biocides, buffers, fluid loss
additives, etc. The wellbores treated can be vertical, deviated or
horizontal. They can be completed with casing and perforations or
open hole.
[0048] A further advantage to the fluids and methods of the
Invention is that they give the operator an additional parameter to
adjust, that is they afford additional flexibility in designing a
treatment that will screen out. Thus in situations in which the
operator may not wish to decrease the pad volume, slow the pumps,
decrease the proppant loading, or make other design changes, he may
add fiber or increase the fiber content. Thus, in the practice of
the Invention, it is preferred to design the treatment so that
screenout would probably occur even without the addition of high
fiber concentrations early in the treatment, and then to add high
fiber concentrations early in the treatment in addition to ensure a
screenout, but it is equally within the scope of the Invention to
design a treatment that probably will not screen out without the
addition of high fiber concentrations early in the treatment, and
then to add high fiber concentrations early in the treatment. It is
also within the scope of this Invention to design and start pumping
a treatment that is not designed or expected to screen out at any
point during the treatment and then during the treatment to decide
to cause the treatment to screen out and therefore at that point to
begin addition of a high fiber concentration or to increase a low
fiber concentration to a high fiber concentration and cause the
screenout (which would not be a tip screenout).
[0049] In gravel packing, or combined fracturing and gravel
packing, it is within the scope of the Invention to apply the
fluids and methods to treatments that are done with or without a
screen. Although we have described the Invention in terms of
hydrocarbon production, it is within the scope of the Invention to
use the fluids and methods in wells intended for the production of
other fluids such as carbon dioxide, water or brine, or in
injection wells. Although we have described the Invention in terms
of unfoamed fluids, fluids foamed or energized (for example with
nitrogen or carbon dioxide or mixtures thereof) may be used.
Adjustment of the appropriate concentrations due to any changes in
the fluid properties or proppant concentration consequent to
foaming would be made. It is also to be understood that the fluids
and methods of the Invention may be used to cause tip screenouts in
multiple fractures or natural fractures.
[0050] It should be pointed out that although it is not desirable
for the screenout to occur in the wellbore, in the annulus between
a screen (if present) and the wellbore face, or in the
perforations, it is desirable that these regions be fully packed at
the end of the job. That is, the desired result is to screen off in
the fracture (the origination of the screenout is in the fracture)
and then to fill (or "pack") the above-mentioned regions with
proppant/gravel.
[0051] Any proppant (gravel) can be used, provided that it is
compatible with the fiber, the formation, the fluid, and the
desired results of the treatment. Such proppants (gravels) can be
natural or synthetic, coated (for example by resin), or contain
chemicals; more than one can be used sequentially or in mixtures of
different sizes or different materials. By proppant we mean any
particulate material selected for a particular purpose such as
propping a fracture to keep it open or gravel packing a completion
to prevent or minimize production of formation fines. Proppants and
gravels in the same or different wells or treatments can be the
same material and/or the same size as one another. Such materials
are usually called proppants when they are placed in fractures and
gravel when they are placed in perforations and wellbores, but the
term "proppant" is intended to include gravel in this discussion.
In general the proppant used will have an average particle size of
from about 10 to about 100 U. S. mesh, more particularly, but not
limited to 40/60, 20/40, 16/20, 12/20 and 8/20 sized materials.
Normally the proppant will be present in the slurry in a
concentration of from about 1 PPA to about 25 PPA, preferably from
about 1 to about 16 PPA.
[0052] Any additives normally used in the pads and proppant-laden
stages of such treatments may be included, again provided that they
are compatible with the other components and the desired results of
the treatment. Such additives can include, but are not limited to
anti-oxidants, crosslinkers, corrosion inhibitors, delay agents,
biocides and buffers. The wellbores treated can be vertical,
deviated or horizontal. They can be completed with casing and
perforations or openhole, and with or without screens.
[0053] Examples of breakers suitable for use in the method of the
present Invention include but are not limited to enzymes such as
galactomannanase (for breaking polysaccharides based on
galactomannan), enzymes such as alpha-amylase for breaking
starches, cellulase and hemi-cellulase for breaking celluloses, and
oxidizers such as persulfates, bromates, iodates, permanganates,
percarbonates, perchlorates, perborates, hypochlorite, chlorine
dioxide, and chlorate (for breaking polymers by oxidation).
Additionally, the breakers can be encapsulated to delay their
release, as is well known in the art. Encapsulation is advantageous
because most or all of the polymer to be broken will be in the
filtercake and, with encapsulation, that is where the breaker will
be late in the job. If the breaker is not encapsulated, at least
some of it will leak off and not be in contact with the polymer in
the filtercake, although some may flow back into contact with the
polymer when the fracture pressure is released. Encapsulation may
also be advantageous because a breaker can be chosen that will
break both the polymer and the micelles in the VES if a VES is
used. Encapsulation is also advantageous for the delayed reaction
it provides. Different breakers are more efficient at different
conditions (especially temperature) and for different viscosifiers,
as is well known in the art.
[0054] Breaker aids (or breaker activators) serve as catalysts to
increase the breaker activity and performance, especially at lower
bottomhole temperatures. Examples are certain tertiary amines, or
mixtures of certain tertiary amines, that are aids for oxidizing
breakers, as described in U.S. Pat. No. 4,560,486.
[0055] It should be understood that breakers and breaker aids may
also be included in job designs for the purpose of degrading the
viscosifying agent in the carrier fluid. These breakers and breaker
aids may be the same as or different from the those included for
the purpose of degrading the filter cake. Degradation of the
viscosifying agent must occur after degradation of the filter cake,
that is the carrier fluid must be capable of transporting proppant
until the treatment has been completed. The choice of breakers, and
breaker aids, and the timing and concentration of the addition of
these and of acid or solvent must be selected accordingly. For
example, a slow acting breaker that is insufficiently active to
degrade the filter cake during the job but sufficiently active to
degrade the viscosifying agent within an acceptable time after
pumping has ceased may be added at any point during a job,
independent of addition of a filter cake degradation agent or
agents or aids. As another example, a breaker aid may be included
in the injected fluid during the time in which the filter cake is
being laid down so that it is incorporated in the filter cake; a
breaker for the viscosifying agent and for the filter cake is added
later in the treatment and because of the breaker aid in the filter
cake, the filter cake is degraded more rapidly than is the
viscosifying agent.
[0056] This Invention may be practiced at any formation
temperature, taking into account any cool-down that may occur, at
which the pad and fracture fluids and their components, in
particular the polymer in the pad and the VES and micelles in the
fracture fluid, have the needed properties, in particular
stability.
EXAMPLE 1
[0057] 1.5 in. diameter cores were saturated in a test brine (2
gallons per thousand gallons of a 50 per cent solution of tetra
methyl ammonium chloride) prior to dynamic fluid loss tests. The
dynamic fluid loss apparatus consists of a core holder designed so
that fluids can be flowed across one end face of the core (the
front end) in such a way that some of the fluid will leak off into
the core, and fluids can be injected into the other end (the back
end) of the core to measure core permeability; the system is
controlled by automation software. Brine was injected into the back
end of the core to measure the initial permeability. Dynamic fluid
loss was performed by flowing a borate crosslinked guar fluid (at a
20 lb guar/1000 gallons of fracturing fluid concentration) across
the face of the core for 30 minutes at a differential pressure of
about 500 psi. (This results in some flow of fluid into the core,
and formation of a filter cake on the core face if there is a
filter cake forming material in the fluid.) An automated fracture
simulator controlled the injection rate to simulate the shear rate
during an actual treatment. The fracture treatment parameters that
the dynamic fluid loss experiments were designed to mimic are
listed in Table 1. Following dynamic leak-off, the regained
permeability was measured by again injecting the same brine into
the back end of the core.
1 TABLE 1 Parameter Treatment value Injection Rate 15 bpm Injection
Time 30 min Power Law Exponent (n') 0.7 Fracture Height 65 ft
Fracture Length 75 ft Fracture Width (At Wellbore) 0.75 in Distance
From Wellbore 1 ft
[0058] The experiments were done at 52.degree. C. Table 2 shows
comparisons of laboratory results of dynamic leak-off tests
simulating fractures with and without an FLA (the FLA concentration
was 30 lbs of fluid loss additive per 1000 gallons of fracturing
fluid); this FLA is a mixture of starch and particulate platelets.
The data show the effects of the FLA on permeability, leak-off and
depth of penetration of leaked-off fluid into the rock. The data
show that fluid loss, both spurt (the amount of leak-off before a
filter cake is formed) and the leak-off after the filter cake was
formed, was much smaller, final permeability was much greater, and
matrix penetration depths by fluid were much smaller when the FLA
was used. These results show how a good FLA will prevent or delay
screenout. The results of tests 2 and 4 are shown graphically in
FIG. 1. Such data would be used in the design of the methods of the
Invention. FIG. 2 (not to scale) demonstrates schematically how the
presence or absence of a filtercake affects the extent to which
fluid leaks off from the fracture into the rock matrix. In FIG. 2,
a filter cake [1] is formed by the FLA in the upper schematic, but
not in the lower, which represents a case in which FLA was not used
or was removed. Consequently, without the filter cake, there is
more leaked off fluid [2] from the propped fracture [3].
2TABLE 2 Initial Final Leak-off after Penetration Perm. Perm. Spurt
Spurt Depth Run (mD) (mD) (gal/100 ft.sup.2) (gal/100 ft.sup.2)
(inches) (Without FLA) 1 98 38 146 72 25 2 80 10 123 58 21 (With
FLA) 3 80 47 46 19 8 4 75 35 60 17 10
EXAMPLE 2
[0059] FIG. 3 shows laboratory experiments demonstrating a method
of the Invention using two FLA breaker (filter cake degradation
agent) stages. These are dynamic fluid loss test runs at 52.degree.
C. by the same method as Example 1. It can be seen that in test one
when the first half contained an FLA and a first breaker and a
breaker aid (filter cake degradation agent aid) for a second
breaker that was present in the second half, and there was still
FLA in the second half, there was no increase in fluid loss in the
second half. In test two, when the first half was like the first
half of test one but the second half contained no FLA, there was a
dramatic increase in the volume of fluid lost in the second half,
indicating that the filter cake had been severely damaged. In a
fracture, this would translate into bridging and/or reduced fluid
efficiency and a TSO. To ensure that the result was not due solely
to the exclusion of the FLA from the second half of test 2, another
laboratory test was run (see FIG. 4) in which there was no breaker
or breaker aid in either stage, but the first stage included the
FLA and the second stage did not. FIG. 4 shows that in this case
there was a slight increase in flow in the second stage, but it was
very minor compared to the results shown in the tests in FIG. 3.
This makes it clear that the major factor was the breakers and
especially the inclusion in the first stage of a breaker aid for
the breaker in the second stage and that leaving the FLA out of the
second stage was of low importance. The first stage of these
experiments represents either the pad or the pad plus the early
proppant stages of a commercial stimulation treatment; the second
stage of these experiments represents the late proppant stages of a
commercial stimulation treatment.
EXAMPLE 3
[0060] FIG. 5 demonstrates the effect of adding fiber to promote
bridging in addition to adding an FLA and breakers. The figure
shows a particular embodiment in which a filter cake with a
built-in breaker is created with the pad, then fibers are added to
the proppant stage to promote bridging, and then another breaker is
added to the later proppant stages. (Schematics A through E of the
contents of the fracture are shown from top to bottom as the
stimulation progresses; these could be either top views or side
views and are not to scale and the fractures are not necessarily
the same size in successive schematics.) This sequence stops the
fracture growth and then removes the filter cake, which ultimately
increases the flow rate, into the fracture, of the fluid to be
produced. The viscosifier in the pad, the first filter cake
degradation agent, the filter cake degradation agent aid for the
second filter cake degradation agent, and the FLA are the same as
those in the first half of test 2 of FIG. 2; the viscosifier in the
carrier fluid is the same as in the pad, and the second filter cake
degradation agent is the same as the one in the second half of test
2 in FIG. 2. In FIG. 5, "2-4 PPA" means the stages containing 2 to
4 pounds of proppant per pound of fluid ("pounds proppant added" or
PPA) and "4 PPA and Up" means the stages from 4 PPA to the last
proppant-containing stage plus a flush.
[0061] The viscosified pad contains the first filter cake
degradation agent, the filter cake degradation agent aid for the
second filter cake degradation agent, and the FLA. As the pad is
pumped (schematic A) and is at the leading edge of the growing
fracture [4], a filter cake [5] is built for fluid loss control and
some fluid leaks off [6] into the formation rock. Enough pad must
be pumped for the filter cake to form. In the 2-4 PPA stages
(schematic B), the carrier fluid contains a synthetic organic
polymeric fiber [7] added to each proppant [8] stage at a
concentration of about 0.6 volume per cent of the liquid in the
slurry that arrests the fracture length growth. In subsequent
stages (schematic C) the second filter cake degradation agent is
introduced and begins to degrade the filter cake, aided by the
filter cake degradation agent aid (that is already present) for the
second filter cake degradation agent. During pumping of the late
proppant-laden stages (schematic D) the second filter cake
degradation agent degrades the filter cake, causing increasingly
greater leak-off. The final result (schematic E) is a relatively
short, wide fracture that has screened off when and where desired,
has little or no filter cake, and is well-packed with proppant.
Many variations on this scheme, for example but not limited to
exactly when and how much of each of the FLA, the first filter cake
degradation agent, the filter cake degradation agent aid for the
second filter cake degradation agent, the second filter cake
degradation agent, and the fiber are added are within the scope of
the Invention. Other variations may include adding the above
materials in different orders or in different combinations.
EXAMPLE 4
[0062] Three fracturing scenarios were simulated with FracCADE.TM.
(Schlumberger proprietary fracture design, prediction and
treatment-monitoring software). In these scenarios, the same FLA,
and when present the same first filter cake degradation agent,
filter cake degradation agent aid for the second filter cake
degradation agent, second filter cake degradation agent, and fiber
as in Example 3 were used. FLA was added in all three scenarios at
a rate designed to form a filter cake of 2 pounds of FLA per one
hundred square feet of fracture surface. The job design is shown in
Table 3. The pump rate was 15 barrels per minute throughout; the
pad and the proppant-laden stages were viscosified with a
boron-crosslinked 20 pounds per thousand gallons guar in sea water;
the flush contained the same guar at the same concentration in sea
water, but uncrosslinked.
3TABLE 3 Fluid Pounds Barrels Minutes Stage gallons Proppant Slurry
Pumping PAD 5500 0 131 8.7 0.5 PPA 1000 500 24.3 1.6 1.0 PPA 1000
1000 24.9 1.7 2.0 PPA 1000 2000 26.0 1.7 4.0 PPA 1000 4000 28.1 1.9
6.0 PPA 1000 6000 30.3 2.0 8.0 PPA 1000 8000 32.4 2.2 10.0 PPA 1500
15000 51.9 3.5 12.0 PPA 3000 36000 110.2 7.3 FLUSH 3286 0 78.2
5.2
[0063] In scenarios 1 and 2, no filter cake degradation agents or
filter cake degradation agent aids were used. In scenario 2, fiber
was added to the 2 to 4 PPA stages at a rate of 0.8 weight per cent
of the proppant. In scenario 3 the pad included a first filter cake
degradation agent and a filter cake degradation agent aid for a
second filter cake degradation agent, and the proppant-laden stages
starting with 2 PPA contained the second filter cake degradation
agent. The results of the three simulations are shown in Table
4.
4 TABLE 4 Scenario: 1 2 3 FLA in Pad? Yes Yes Yes Filter Cake No No
Yes Degradation Agents and Aid Used? Pad Spurt (gal/100 ft.sup.2) 0
0 46 Fiber in 2-4 PPA No Yes No Stages? Proppant Stages Spurt 0 0
99 (gal/100 ft.sup.2) Final Propped Fracture 55.3 45.4 36.9 Half
Length Final Propped Fracture 1.298 1.729 3.052 Width at
Wellbore
[0064] Note that the design included sufficient pumping time to
ensure filter cake formation. Amounts of pad, fracture fluid,
fracture fluid viscosifier, breaker (filter cake degradation
agent), breaker aid (filter cake degradation agent aid), fluid loss
control additive, and proppant typical of commercial treatments
were used. It can be seen from scenario I that when an FLA was used
but no means for destroying the filter cake was employed, a long
narrow fracture was produced. When fiber was added to promote a tip
screenout in scenario 2, a shorter, wider fracture was created.
When filter cake degradation was used to promote the tip screenout,
the shortest, widest fracture was created. A good job design would
be a combination of scenarios 2 and 3.
[0065] The preceding description of specific embodiments of the
present Invention is not intended to be a complete list of every
possible embodiment of the Invention. Persons skilled in this field
will recognize that modifications can be made to the specific
embodiments described here that would be within the scope of the
present Invention.
* * * * *